Non-steady state reactor and method for producing synthesis gas
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A technology of reactor and synthesis gas, which is applied in gas fuel, petroleum industry, fuel and other directions, can solve the problems of spontaneous combustion and explosion danger, difficulty in controlling the temperature of the reactor bed, and easy flameout of the reactor.
Active Publication Date: 2013-01-30
SYNFUELS CHINA TECH CO LTD
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However, there are insurmountable problems in this reactor: there is a high-temperature hot zone in the catalytic bed of the reactor, there is a risk of spontaneous combustion and explosion when the feed preheating temperature is high, the reactor is easy to extinguish, and the bed temperature is difficult to control, etc., so it is difficult to realize industrialization
Since the catalytic partial oxidation of methane on the nickel-based catalyst is divided into two steps: fast oxidation and slow reforming, it is difficult to avoid high-temperature hot spots in the reactor bed. (Catalytic partial oxidation usually adopts mixed feed of raw material gas and oxidant), and the feed cannot be preheated to a very high temperature in the heat storage section, which not only makes it difficult to control the temperature of the reactor bed, but also affects the thermal efficiency of the process and the synthesis gas recovery. Rate
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Embodiment 1
[0101] Examples 1 and 2 are both in figure 1 In the reactor device shown, the coal-based Fischer-Tropsch synthesis tail gas (TG) is used as a raw material to produce synthesis gas, and the molar composition of the coal-based Fischer-Tropsch synthesis tail gas raw material is CH 4 25%, CO 20%, H 2 30%, CO 2 20%, N 2 5%. The catalyst used in the reforming section of the reactor is a commercial steam reforming nickel catalyst; the heat storage section is filled with porcelain Raschig rings. The reactions and results are as follows:
[0102] The inlet flow rate of the raw material gas is 1000 kmol / hr, the pressure is 25 bar, and the temperature is 300°C; the optimal bypass feed ratio of the raw material gas is 0.38, that is, 62% of the raw material gas enters the combustion chamber through the burner along L11, and the other 38% of the raw material The gas enters the reactor from the bypass line L5 or L6 at the bottom of the reactor after being adjusted by the flow direction swit...
Embodiment 2
[0110] Using coke oven gas (COG) as the raw material, using the same method as in Example 1, a regenerative autothermal reforming experiment to produce synthesis gas was carried out. The results are as follows:
[0111] Coke oven gas composition is CH 4 32%, CO 9%, H 2 52%, CO 2 3%, N 2 3.7%, O 2 0.3%, the feed flow rate is 1000 kmol / hr, the best bypass feed ratio is 0.33; the oxygen feed flow rate is 190 kmol / hr, feed O 2 / CH 4 0.59; Bypass steam feed flow rate is 600kmol / hr, H in feed 2 O / CH 4 The ratio is 1.87.
[0112] The half cycle time of the forced flow direction change of the reactor is 5 minutes.
[0113] After the reactor started up, it took about 32 changes in flow direction to reach a periodic steady state.
[0114] After the reactor reaches a periodic steady state, the temperature at the outlet of the feed preheating storage section fluctuates from 984°C to 973°C, and the hourly average value is 982°C; the temperature at the outlet of the complete reforming section f...
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Abstract
The invention discloses a reactor device and method for producing synthesis gas by using gaseous hydrocarbon as a raw material for carrying out heat accumulating type self-heating conversion. The reactor mainly comprises a combustion chamber, a mixing chamber, two reforming sections and two heat accumulating sections. The feeding raw gas of the reactor is divided into two paths of gas, wherein one path of raw gas and oxygen gas enter the combustion chamber from a middle combustion nozzle to carry out heat generating reaction; and after the other path of raw gas is mixed with water vapor, the mixed gas laterally enters the reactor through a gas inlet at one end, the mixed gas carries out pre-reforming reaction in one reforming section after being preheated in one heat accumulating section, the gas after reaction is mixed with the high-temperature gas at the outlet of the combustion chamber, then the mixed gas enters the other reforming section to carry out reforming reaction, and products are discharged after being cooled by the other heat accumulating section. The reactor of the invention is matched with a flow direction switching valve capable of periodically changing the flow direction of the gas in the reactor, thus the purposes of preheating feed materials, carrying out reaction and cooling products in one reactor can be realized. The reactor of the invention can reduce the oxygen consumption in the process, improve the yield and the quality of the synthesis gas and improve the heat efficiency of the overall process.
Description
Technical field [0001] The present invention relates to a device and method for producing synthesis gas; further, the synthesis gas production device includes an unsteady state reactor and its supporting facilities; the synthesis gas production method uses gaseous hydrocarbons as raw materials, Under unsteady state conditions, syngas is produced through regenerative autothermal conversion. Background technique [0002] The gaseous hydrocarbon feedstock in the present invention refers to a gas mixture whose main components are gaseous alkanes or olefins, such as natural gas, coke oven gas, refinery gas, Fischer-Tropsch synthesis tail gas, coal bed methane and the like. Generally, such gaseous hydrocarbon feedstocks can be converted into synthesis gas (a mixture of hydrogen and carbon monoxide) through processes such as catalytic steam reforming, non-catalytic partial oxidation, and autothermal reforming to produce liquid fuels or chemicals, synthetic methanol, and synthetic ammoni...
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